CN111632492A - Medium and low temperature SCR denitration ammonia injection system - Google Patents
Medium and low temperature SCR denitration ammonia injection system Download PDFInfo
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- CN111632492A CN111632492A CN202010636600.2A CN202010636600A CN111632492A CN 111632492 A CN111632492 A CN 111632492A CN 202010636600 A CN202010636600 A CN 202010636600A CN 111632492 A CN111632492 A CN 111632492A
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- flue gas
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 287
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 137
- 238000002347 injection Methods 0.000 title claims abstract description 42
- 239000007924 injection Substances 0.000 title claims abstract description 42
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 197
- 239000003546 flue gas Substances 0.000 claims abstract description 197
- 238000005507 spraying Methods 0.000 claims abstract description 90
- 238000001704 evaporation Methods 0.000 claims abstract description 77
- 230000008020 evaporation Effects 0.000 claims abstract description 77
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims abstract description 50
- 235000011114 ammonium hydroxide Nutrition 0.000 claims abstract description 50
- 239000007921 spray Substances 0.000 claims abstract description 47
- 238000007789 sealing Methods 0.000 claims description 20
- 239000000779 smoke Substances 0.000 claims description 13
- 230000009977 dual effect Effects 0.000 claims 4
- 230000000694 effects Effects 0.000 abstract description 8
- 238000000746 purification Methods 0.000 abstract description 2
- 239000000571 coke Substances 0.000 description 10
- 238000010586 diagram Methods 0.000 description 8
- 238000002309 gasification Methods 0.000 description 5
- 238000012423 maintenance Methods 0.000 description 5
- 239000003054 catalyst Substances 0.000 description 3
- 239000003638 chemical reducing agent Substances 0.000 description 3
- 230000007547 defect Effects 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 238000004088 simulation Methods 0.000 description 2
- 230000008646 thermal stress Effects 0.000 description 2
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 239000004202 carbamide Substances 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8621—Removing nitrogen compounds
- B01D53/8625—Nitrogen oxides
- B01D53/8631—Processes characterised by a specific device
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/20—Reductants
- B01D2251/206—Ammonium compounds
- B01D2251/2062—Ammonia
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
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- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention relates to the technical field of flue gas purification, in particular to a medium-low temperature SCR denitration ammonia spraying system. Denitration ammonia injection system includes: an ammonia water storage tank; the spray gun is connected with an ammonia outlet of the ammonia water storage tank; the two-stage rotational flow ammonia spraying evaporation device is connected with the outlet of the spray gun, and the bottom of the two-stage rotational flow ammonia spraying evaporation device is provided with a high-temperature flue gas inlet; the high-temperature flue gas outlet is connected with the high-temperature flue gas inlet of the two-stage rotational flow ammonia spraying evaporation device; the mixer is connected with the ammonia-containing flue gas inlet and the flue gas outlet of the two-stage rotational flow ammonia spraying evaporation device; the mixer is also provided with an original flue gas inlet; the hot flue gas outlet is connected with the raw flue gas inlet of the mixer; the flue gas inlet is connected with the flue gas outlet of the mixer; and a flue gas outlet of the SCR denitration reactor is connected with a hot flue gas inlet of the flue gas heat exchanger. The denitration ammonia injection system is simple in structure, excellent in mixing effect of ammonia gas and raw flue gas and small in denitration flue gas resistance.
Description
Technical Field
The invention relates to the technical field of flue gas purification, in particular to a medium-low temperature SCR denitration ammonia spraying system.
Background
The raw flue gas temperature of the medium-low temperature SCR denitration process is low, in order to ensure proper operation temperature, the raw flue gas needs to be heated for the first time through a flue gas heat exchanger, then the raw flue gas is mixed with high-temperature flue gas generated by a hot blast stove for the second time, and a denitration reducing agent (commonly used ammonia water, liquid ammonia, urea and the like) selectively reacts with NOx in the flue gas under the condition of a catalyst to generate nitrogen and water, so that the NOx in the flue gas is removed. The injection and mixing of denitration reducing agent is an important component of the whole system, the existing ammonia injection system is generally ejected from an ammonia water storage tank, gasified by an evaporator (or other evaporation device), mixed with high-temperature flue gas by an injection grid arranged on an SCR inlet flue, and fed into an SCR denitration reactor for denitration reaction, and the flow chart of the system is shown in FIG. 1. However, the ammonia injection system is high in cost, the injection grid pipe is easy to wear and block, and meanwhile, dust in flue gas is easy to accumulate near the nozzle, so that the denitration efficiency is influenced.
According to the cyclone mixing device for the SCR flue gas denitration system disclosed by the Chinese patent CN103657411A, ammonia water is gasified through an external evaporator (or other evaporation devices), is sprayed into a vertical flue of an SCR inlet through a group of ammonia nozzles, and then is mixed with flue gas through the cyclone mixing device on one elevation surface. The cyclone mixing device is arranged on the SCR inlet flue, the section of the SCR inlet flue is large, and a large number of cyclone mixer groups need to be arranged, so that the investment cost is increased, and the defect that the overhaul is difficult when an ammonia injection pipeline is blocked exists.
The ammonia gas and flue gas mixing device of the double-stage rotary SCR denitration system disclosed in the Chinese patent CN102228794A is characterized in that ammonia water is gasified by an external evaporator (or other evaporation device) and is sprayed into a vertical flue of an SCR inlet by an ammonia gas injection pipe. According to the invention, two stages of mixing discs are arranged in the flue in a staggered manner from front to back, and the mixing discs are fixedly connected with the flue wall plate through the disc box connecting mixing rods, so that although flue gas can be in two sets of rotary flow states, dead corners are eliminated, the defects of inconvenience in installation, high cost and difficulty in overhauling when a pipeline is blocked are not solved.
It can be seen that the existing denitration ammonia injection system has the following defects:
1) most of the existing ammonia spraying systems gasify ammonia water through an evaporator (or other evaporation devices), spray the gasified ammonia water into a vertical flue of an SCR inlet through a spraying grid, and mix the gasified ammonia water with flue gas through a mixing device, but the mixing device has a complex structure and is inconvenient to install, so that the investment cost is high.
2) The current ammonia system that spouts into the vertical flue of SCR import through spraying grid or injection pipe, and the pipeline is more and little, appears wearing and tearing and blocking phenomenon easily, and the dust in the flue gas is very easy to pile up near the nozzle, just has the dead angle simultaneously, leads to ammonia and former flue gas mixing effect relatively poor, and then seriously influences denitration efficiency.
Disclosure of Invention
In view of this, the technical problem to be solved by the present invention is to provide a medium and low temperature SCR denitration ammonia injection system with a simple structure, which has a better mixing effect of ammonia gas and raw flue gas and a small resistance to denitration flue gas.
The invention provides a medium-low temperature SCR denitration ammonia spraying system, which comprises:
an ammonia water storage tank;
the spray gun is connected with an ammonia outlet of the ammonia water storage tank;
the two-stage rotational flow ammonia spraying evaporation device is connected with the outlet of the spray gun, and the bottom of the two-stage rotational flow ammonia spraying evaporation device is provided with a high-temperature flue gas inlet;
the high-temperature flue gas outlet is connected with the high-temperature flue gas inlet of the two-stage rotational flow ammonia spraying evaporation device;
the mixer is connected with the ammonia-containing flue gas inlet and the flue gas outlet of the two-stage rotational flow ammonia spraying evaporation device; the mixer is also provided with an original flue gas inlet;
the hot flue gas outlet is connected with the raw flue gas inlet of the mixer;
the flue gas inlet is connected with the flue gas outlet of the mixer; and a flue gas outlet of the SCR denitration reactor is connected with a hot flue gas inlet of the flue gas heat exchanger.
Preferably, the two-stage cyclone ammonia injection evaporation device comprises:
a cavity;
the bottom to the top of cavity set gradually: a divergent section, a mixing section and a convergent section;
a first-stage rotational flow device is arranged on the divergent section;
a second-stage rotational flow device is arranged at the mixing section;
the bottom of the cavity is provided with a high-temperature flue gas inlet; the top of the cavity is provided with a smoke outlet;
and an ammonia spraying port is arranged on the side wall of the cavity of the mixing section.
Preferably, the distance of the divergent section is 0.1-1 times of the equivalent diameter of the mixing section;
the distance between the mixing sections is 2-5 times of the equivalent diameter of the mixing sections;
the distance of the reducing section is 0.1-1 times of the equivalent diameter of the mixing section.
Preferably, the primary cyclone device comprises a first inner ring support (4-1-1), first cyclone blades (4-1-2), a first outer ring support (4-1-3), first support blades (4-1-4) and a first closing plate (4-1-5);
the first inner ring support (4-1-1) and the first outer ring support (4-1-3) are coaxially arranged, the first rotational flow blades (4-1-2) are uniformly distributed in the area between the first inner ring support (4-1-1) and the first outer ring support (4-1-3) along the circumferential direction by taking the first inner ring support (4-1-1) as an axis, and two ends of the first rotational flow blades (4-1-2) are fixedly connected to the first inner ring support (4-1-1) and the first outer ring support (4-1-3) respectively; the inclination angles of the first rotational flow blades (4-1-2) and the first inner ring support (4-1-1) are 10-80 degrees, and the blade inclination angles of the first rotational flow blades (4-1-2) are all equal;
the first supporting blades (4-1-4) are uniformly distributed on one side, far away from the first swirl blades (4-1-2), of the first outer ring support (4-1-3) along the circumferential direction; the first supporting blade (4-1-4) is positioned on a plane formed by the first inner ring support (4-1-1) and the first outer ring support (4-1-3); one side of the first supporting blade (4-1-4) close to the first outer ring support (4-1-3) is fixedly connected with the first outer ring support (4-1-3); one side of the first supporting blade (4-1-4) far away from the first outer ring support (4-1-3) is fixedly connected with the side wall of the cavity of the divergent section;
the first sealing plate (4-1-5) is in threaded connection with the first inner ring support (4-1-1); or the first closing plate (4-1-5) is welded with the first inner ring support (4-1-1).
Preferably, the number of the first swirl vanes is 3-18;
the number of the first supporting blades is 3-16.
Preferably, the included angle between the first supporting blade and the first rotational flow blade is 0-180 degrees.
Preferably, the secondary cyclone device comprises a second inner ring support (4-2-1), second cyclone blades (4-2-2), a second outer ring support (4-2-3), second support blades (4-2-4) and a second closing plate (4-2-5);
the second inner ring support (4-2-1) and the second outer ring support (4-2-3) are coaxially arranged, the second swirl vanes (4-2-2) are uniformly distributed in the area between the second inner ring support (4-2-1) and the second outer ring support (4-2-3) along the circumferential direction by taking the second inner ring support (4-2-1) as an axis, and two ends of each second swirl vane (4-2-2) are fixedly connected to the second inner ring support (4-2-1) and the second outer ring support (4-2-3) respectively; the inclination angles of the second swirl blades (4-2-2) and the second inner ring support (4-2-1) are 10-80 degrees, and the blade inclination angles of the second swirl blades (4-2-2) are all equal;
the second supporting blades (4-2-4) are uniformly distributed on one side, far away from the second swirl blades (4-2-2), of the second outer ring support (4-2-3) along the circumferential direction; the second supporting blade (4-2-4) is positioned on a plane formed by the second inner ring support (4-2-1) and the second outer ring support (4-2-3); one side of the second supporting blade (4-2-4) close to the second outer ring support (4-2-3) is fixedly connected with the second outer ring support (4-2-3); one side of the second supporting blade (4-2-4) far away from the second outer ring support (4-2-3) is fixedly connected with the side wall of the cavity of the mixing section;
the second sealing plate (4-2-5) is in threaded connection with the second inner ring support (4-2-1); or the second closing plate (4-2-5) is welded with the second inner ring support (4-2-1).
Preferably, the number of the second swirl vanes is 3-18;
the number of the second supporting blades is 3-16.
Preferably, the included angle between the second supporting blade and the second rotational flow blade is 0-180 degrees.
Preferably, the number of the ammonia spraying openings is the same as that of the spray guns;
the spray gun is fixed on the ammonia spraying port through a spray gun mounting seat;
the number of the spray guns is 2-3.
The invention provides a medium-low temperature SCR denitration ammonia spraying system, which comprises: an ammonia water storage tank; the spray gun is connected with an ammonia outlet of the ammonia water storage tank; the two-stage rotational flow ammonia spraying evaporation device is connected with the outlet of the spray gun, and the bottom of the two-stage rotational flow ammonia spraying evaporation device is provided with a high-temperature flue gas inlet; the high-temperature flue gas outlet is connected with the high-temperature flue gas inlet of the two-stage rotational flow ammonia spraying evaporation device; the mixer is connected with the ammonia-containing flue gas inlet and the flue gas outlet of the two-stage rotational flow ammonia spraying evaporation device; the mixer is also provided with an original flue gas inlet; the hot flue gas outlet is connected with the raw flue gas inlet of the mixer; the flue gas inlet is connected with the flue gas outlet of the mixer; and a flue gas outlet of the SCR denitration reactor is connected with a hot flue gas inlet of the flue gas heat exchanger. According to the invention, an evaporator (or other evaporation devices) is not needed, a jet grid is not needed, the rapid evaporation and gasification of ammonia water are further realized through a unique two-stage rotational flow ammonia-spraying evaporation device, the ammonia water is fully mixed with high-temperature flue gas, the temperature rise can be uniformly realized with the original flue gas through a flue gas mixer, the large temperature gradient and the thermal stress difference in an SCR inlet flue are avoided, and the temperature deviation of the mixed flue gas in the SCR denitration reactor can reach the +/-5 ℃ requirement and is far higher than the existing standard requirement; and the denitration flue gas resistance is small. Meanwhile, the ammonia spraying device is simple in structure, low in position, easy to operate and low in cost, and solves the problem of difficulty in maintenance.
Drawings
FIG. 1 is a system flow diagram of a prior art ammonia injection system;
FIG. 2 is a flow chart of a medium and low temperature SCR denitration ammonia injection system according to an embodiment of the present invention;
FIG. 3 is a schematic structural diagram of a two-stage cyclone ammonia injection evaporation device according to an embodiment of the present invention;
FIG. 4 is a distance label graph provided in accordance with an embodiment of the present invention;
FIG. 5 is a schematic structural diagram of a primary cyclone device provided in an embodiment of the present invention;
fig. 6 is a schematic structural diagram of a two-stage swirling device according to an embodiment of the present invention.
Detailed Description
The technical solutions of the present invention will be described clearly and completely with reference to the following embodiments of the present invention, and it should be understood that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
The invention provides a medium-low temperature SCR denitration ammonia spraying system, which comprises:
an ammonia water storage tank;
the spray gun is connected with an ammonia outlet of the ammonia water storage tank;
the two-stage rotational flow ammonia spraying evaporation device is connected with the outlet of the spray gun, and the bottom of the two-stage rotational flow ammonia spraying evaporation device is provided with a high-temperature flue gas inlet;
the high-temperature flue gas outlet is connected with the high-temperature flue gas inlet of the two-stage rotational flow ammonia spraying evaporation device;
the mixer is connected with the ammonia-containing flue gas inlet and the flue gas outlet of the two-stage rotational flow ammonia spraying evaporation device; the mixer is also provided with an original flue gas inlet;
the hot flue gas outlet is connected with the raw flue gas inlet of the mixer;
the flue gas inlet is connected with the flue gas outlet of the mixer; and a flue gas outlet of the SCR denitration reactor is connected with a hot flue gas inlet of the flue gas heat exchanger.
Fig. 2 is a flow chart of a medium-low temperature SCR denitration ammonia injection system according to an embodiment of the present invention. Wherein, 1 is the gas heater, 2 is the aqueous ammonia storage tank, 3 is the spray gun, 4 is doublestage whirl spraying ammonia evaporation plant, 5 is the hot-blast furnace, 6 is the blender, 7 is SCR denitration reactor.
The medium-low temperature SCR denitration ammonia spraying system provided by the invention comprises an ammonia water storage tank 2. The ammonia water storage tank is used for storing denitration reducing agent ammonia water. The structure of the ammonia water storage tank is not particularly limited, and the ammonia water storage tank can be generally commercially available. In certain embodiments of the present invention, the concentration of the ammonia water in the ammonia water storage tank is 10 wt% to 25 wt%. In certain embodiments, the aqueous ammonia concentration is 20 wt%.
The medium-low temperature SCR denitration ammonia spraying system provided by the invention further comprises a spray gun 3 connected with an ammonia outlet of the ammonia water storage tank. The spray gun can spray ammonia water into the two-stage rotational flow ammonia spraying evaporation device in an atomized state. The structure of the spray gun is not particularly limited in the present invention, and may be a commercially available atomizing spray gun.
The medium-low temperature SCR denitration ammonia spraying system also comprises a two-stage rotational flow ammonia spraying evaporation device 4 connected with the outlet of the spray gun. And a high-temperature flue gas inlet is arranged at the bottom of the two-stage rotational flow ammonia spraying evaporation device.
In some embodiments of the invention, the two-stage cyclonic ammonia injection evaporation apparatus comprises:
a cavity;
the bottom to the top of cavity set gradually: a divergent section, a mixing section and a convergent section;
a first-stage rotational flow device is arranged on the divergent section;
a second-stage rotational flow device is arranged at the mixing section;
the bottom of the cavity is provided with a high-temperature flue gas inlet; the top of the cavity is provided with a smoke outlet;
and an ammonia spraying port is arranged on the side wall of the cavity of the mixing section.
Fig. 3 is a schematic structural diagram of a two-stage cyclone ammonia injection evaporation device according to an embodiment of the present invention.
In certain embodiments of the invention, the distance of the diverging section is 0.1 to 1 times the equivalent diameter of the mixing section. In certain embodiments, the distance of the diverging section is 0.61 or 0.55 times the equivalent diameter of the mixing section. In certain embodiments of the present invention, the distance of the mixing section is 2 to 5 times the equivalent diameter of the mixing section. In certain embodiments, the distance of the mixing section is 4.8 or 3.7 times the equivalent diameter of the mixing section. In certain embodiments of the present invention, the distance of the tapered sections is 0.1 to 1 times the equivalent diameter of the mixing section. In certain embodiments, the distance of the tapered section is 0.61 or 0.47 times the equivalent diameter of the mixing section. Referring to fig. 4, fig. 4 is a distance labeled diagram provided by an embodiment of the invention. Wherein a is the distance of the divergent section or the height of the divergent section, b is the distance of the mixing section or the height of the mixing section, and c is the distance of the convergent section or the height of the convergent section.
In some embodiments of the invention, the cavity portion of the mixing section is cylindrical, as shown in fig. 3. In certain embodiments, the cavity portion of the mixing section is rectangular parallelepiped.
In some embodiments of the invention, the diameter of the upper surface of the top of the cavity is 0.3 to 0.9 times the equivalent diameter of the mixing section. In certain embodiments, the diameter of the top surface of the cavity top is 0.7 times the mixing section equivalent diameter.
In some embodiments of the invention, the diameter of the lower surface of the bottom of the cavity is 0.3 to 0.9 times the equivalent diameter of the mixing section. In certain embodiments, the diameter of the bottom lower surface of the cavity is 0.8 times or 0.7 times the equivalent diameter of the mixing section.
In some embodiments of the invention, the primary swirler means comprises a first inner ring support 4-1-1, first swirler vanes 4-1-2, a first outer ring support 4-1-3, first support vanes 4-1-4 and a first closing plate 4-1-5;
the first inner ring support 4-1-1 and the first outer ring support 4-1-3 are coaxially arranged, the first swirl vane 4-1-2 takes the first inner ring support 4-1-1 as an axis and is uniformly distributed in an area between the first inner ring support 4-1-1 and the first outer ring support 4-1-3 along the circumferential direction, and two ends of the first swirl vane 4-1-2 are fixedly connected to the first inner ring support 4-1-1 and the first outer ring support 4-1-3 respectively; the inclination angles of the first swirl blades 4-1-2 and the first inner ring support 4-1-1 are 10-80 degrees, and the blade inclination angles of the first swirl blades 4-1-2 are all equal;
the first supporting blades 4-1-4 are uniformly distributed on one side of the first outer ring support 4-1-3 far away from the first swirl blades 4-1-2 along the circumferential direction; the first supporting blade 4-1-4 is positioned on a plane formed by the first inner ring support 4-1-1 and the first outer ring support 4-1-3; one side of the first supporting blade 4-1-4 close to the first outer ring support 4-1-3 is fixedly connected with the first outer ring support 4-1-3; one side of the first supporting blade 4-1-4, which is far away from the first outer ring support 4-1-3, is fixedly connected with the side wall of the cavity of the divergent section;
the first sealing plate 4-1-5 is in threaded connection with the first inner ring support 4-1-1, or the first sealing plate (4-1-5) is welded with the first inner ring support (4-1-1) and used for sealing a central hole of the first inner ring support 4-1-1.
Fig. 5 is a schematic structural diagram of a primary cyclone device according to an embodiment of the present invention.
In some embodiments of the invention, the first swirl vanes are angled at 45 ° to the first inner ring support axis.
In some embodiments of the present invention, the number of the first swirl vanes is 3 to 18. In certain embodiments, the number of first swirl vanes is 8.
In some embodiments of the present invention, the number of the first supporting blades is 3 to 16. In some embodiments, the number of the first support blades is 8.
In some embodiments of the present invention, the first support blade and the first swirl blade form an angle of 0 ° to 180 °. In some embodiments, the first support vane is angled 45 ° from the first swirl vane.
In certain embodiments of the present invention, the diameter of the first inner ring support 4-1-1 is 0.05 to 0.5 times the equivalent diameter of the mixing section. In certain embodiments, the diameter of the first inner ring support 4-1-1 is 0.15 times or 0.11 times the mixing section equivalent diameter. In certain embodiments of the invention, the diameter of the first outer ring support 4-1-3 is 0.3 to 0.8 times the equivalent diameter of the mixing section. In certain embodiments, the diameter of the first outer ring support 4-1-3 is 0.6 times the mixing section equivalent diameter.
In some embodiments of the invention, the distance from the first-stage cyclone device to the bottom of the divergent section is 0.2-0.5 times of the distance from the divergent section. In some embodiments, the distance from the primary cyclone device to the bottom of the divergent section is 0.35 times the distance of the divergent section.
In some embodiments of the present invention, the secondary swirler means comprises a second inner ring support 4-2-1, second swirler vanes 4-2-2, a second outer ring support 4-2-3, second support vanes 4-2-4, and a second closing plate 4-2-5;
the second inner ring support 4-2-1 and the second outer ring support 4-2-3 are coaxially arranged, the second swirl vanes 4-2-2 are uniformly distributed in the area between the second inner ring support 4-2-1 and the second outer ring support 4-2-3 along the circumferential direction by taking the second inner ring support 4-2-1 as an axis, and two ends of the second swirl vanes 4-2-2 are fixedly connected to the second inner ring support 4-2-1 and the second outer ring support 4-2-3 respectively; the inclination angles of the second swirl blades 4-2-2 and the second inner ring support 4-2-1 are 10-80 degrees, and the blade inclination angles of the second swirl blades 4-2-2 are all equal;
the second supporting blades 4-2-4 are uniformly distributed on one side of the second outer ring support 4-2-3 far away from the second swirl blades 4-2-2 along the circumferential direction; the second supporting blade 4-2-4 is positioned on a plane formed by the second inner ring support 4-2-1 and the second outer ring support 4-2-3; one side of the second supporting blade 4-2-4 close to the second outer ring support 4-2-3 is fixedly connected with the second outer ring support 4-2-3; one side of the second supporting blade 4-2-4, which is far away from the second outer ring support 4-2-3, is fixedly connected with the side wall of the cavity of the mixing section;
the second sealing plate (4-2-5) is in threaded connection with the second inner ring support (4-2-1), or the second sealing plate (4-2-5) is welded with the second inner ring support (4-2-1) and used for sealing a central hole of the second inner ring support (4-2-1).
The first sealing plate 4-1-5 and the second sealing plate 4-2-5 are arranged to prevent the smoke from directly passing through the central hole, so that the cyclone effect of the smoke is enhanced.
Fig. 6 is a schematic structural diagram of a two-stage swirling device according to an embodiment of the present invention.
In some embodiments of the invention, the second swirl vanes are angled at 45 ° to the second inner ring support axis.
In some embodiments of the present invention, the number of the second swirl vanes is 3 to 18. In certain embodiments, the number of second swirl vanes is 8.
In some embodiments of the present invention, the number of the second supporting blades is 3 to 16. In some embodiments, the number of the second support blades is 8.
In some embodiments of the invention, the second support blade and the second swirl blade form an angle of 0 ° to 180 °. In some embodiments, the second support vane is angled 45 ° from the second swirl vane.
In certain embodiments of the invention, the diameter of the second inner ring support 4-2-1 is 0.05 to 0.5 times the equivalent diameter of the mixing section. In certain embodiments, the diameter of the second inner ring support 4-2-1 is 0.15 times or 0.11 times the mixing section equivalent diameter. In certain embodiments of the invention, the diameter of the second outer ring support 4-2-3 is 0.3 to 0.8 times the equivalent diameter of the mixing section. In certain embodiments, the diameter of the second outer ring support 4-2-3 is 0.6 times the mixing section equivalent diameter.
In some embodiments of the invention, the distance from the secondary cyclone device to the top of the mixing section is 0.1-1 times the equivalent diameter of the mixing section. In certain embodiments, the distance from the secondary swirl device to the top of the mixing section is 0.7 or 0.8 times the mixing section equivalent diameter.
In the invention, the first-stage cyclone device and the second-stage cyclone device are two-stage cyclone devices with different elevations, but not cyclone devices on the same plane, and the mixing is realized through two-stage cyclones with different elevations, so that the mixing effect is better.
The arrangement of the ammonia injection port is not particularly limited in the present invention. In some embodiments of the present invention, the number of the ammonia injection openings is 2-3. In some embodiments of the invention, the ammonia injection ports are arranged at a uniform angle on a plane. In some embodiments of the present invention, the distance from the ammonia injection port to the bottom of the mixing section is 0.05 to 0.5 times the equivalent diameter of the mixing section. In certain embodiments, the distance from the ammonia injection port to the bottom of the mixing section is 0.2 times or 0.15 times the equivalent diameter of the mixing section.
In some embodiments of the invention, the number of the spray guns is the same as the number of the ammonia injection ports.
In certain embodiments of the invention, the lance is secured to the ammonia injection port by a lance mount. The structure of the spray gun mounting seat is not particularly limited, and the spray gun mounting seat can be generally commercially available.
In some embodiments of the invention, the two-stage cyclone ammonia-spraying evaporation device further comprises a standby spray gun mounting seat, and when one spray gun has a problem, the standby spray gun can be quickly started to realize the function of online maintenance.
In some embodiments of the present invention, the number of the spray guns is 2 to 3. 2-3 spray guns are arranged around the double-stage rotational flow ammonia spraying evaporation device, so that the mixing effect is improved.
The medium and low temperature SCR denitration ammonia spraying system provided by the invention also comprises a hot blast stove 5. And a high-temperature flue gas outlet of the hot blast stove is connected with a high-temperature flue gas inlet of the two-stage rotational flow ammonia spraying evaporation device. The structure of the hot blast stove is not particularly limited, and the hot blast stove can be a common commercial hot blast stove. In certain embodiments of the invention, the temperature of the high temperature flue gas exiting the hot blast stove is 800 ℃.
High temperature flue gas that the hot-blast furnace produced gets into from doublestage whirl spraying ammonia evaporation plant lower part, reduce the velocity of flow (providing abundant time for aqueous ammonia gasification and evaporation) through the gradual expanding section earlier, simultaneously through one-level whirl device, high temperature flue gas is the whirl form and rises, and the aqueous ammonia is atomized form by the spray gun and spouts into, meet the high temperature flue gas of whirl form, the aqueous ammonia is the ammonia in the twinkling of an eye gasification, along with the flue gas flows, through the mixture of mixing section, rethread second grade whirl device, the intensive mixing, then resume original velocity of flow through the convergent section.
The medium-low temperature SCR denitration ammonia spraying system provided by the invention also comprises a mixer 6. The mixer is provided with an ammonia-containing flue gas inlet, a raw flue gas inlet and a flue gas outlet. And an ammonia-containing flue gas inlet of the mixer is connected with a flue gas outlet of the two-stage rotational flow ammonia spraying evaporation device. In some embodiments of the present invention, the mixer is a flue gas mixing and heating device, specifically a flue gas mixing and heating device manufactured by fujianlong desulfurization and denitration engineering ltd, such as the flue gas mixing and heating device described in patent publication No. CN 209752619.
In some embodiments of the present invention, the ammonia-containing flue gas inlet of the mixer is disposed on the side wall of the mixer, and the present invention is not limited to this arrangement.
The medium-low temperature SCR denitration ammonia spraying system provided by the invention further comprises a flue gas heat exchanger 1. The flue gas heat exchanger is provided with a raw flue gas inlet, a hot flue gas outlet, a hot flue gas inlet and a cold flue gas outlet. And a hot flue gas outlet of the flue gas heat exchanger is connected with a raw flue gas inlet of the mixer. The structure of the flue gas heat exchanger is not particularly limited, and the flue gas heat exchanger can be generally commercially available. In certain embodiments of the invention, the hot flue gas temperature after heat exchange in the flue gas heat exchanger 1 is 230 ℃.
The medium and low temperature SCR denitration ammonia spraying system provided by the invention also comprises an SCR denitration reactor 7. The SCR denitration reactor is provided with a flue gas inlet and a flue gas outlet. And a flue gas inlet of the SCR denitration reactor is connected with a flue gas outlet of the mixer. And a flue gas outlet of the SCR denitration reactor is connected with a hot flue gas inlet of the flue gas heat exchanger. The structure of the SCR denitration reactor is not particularly limited, and may be generally commercially available.
When the medium-low temperature SCR denitration ammonia spraying system provided by the invention is used for denitration, raw flue gas is firstly heated by the flue gas heat exchanger 1 for the first time, ammonia water is sprayed out from the ammonia water storage tank 2 and sprayed into the two-stage rotational flow ammonia spraying evaporation device 4 by the spray gun 3, meanwhile, high-temperature flue gas generated by the hot blast stove 5 also enters the two-stage rotational flow ammonia spraying evaporation device 4, the ammonia water is instantly evaporated and is firstly mixed with the high-temperature flue gas, the raw flue gas is fully heated for the second time by the mixer 6, the ammonia gas and the flue gas are mixed, and finally the mixture enters the SCR denitration reactor 7 for denitration reaction, and the flue gas after denitration can be discharged to a chimney after being cooled by the flue gas heat exchanger 1. The medium-low temperature SCR denitration ammonia spraying system fully utilizes the temperature of high-temperature flue gas, ammonia water can be directly gasified into ammonia gas, so that an evaporator is saved, the function of an original flue gas mixer is added, ammonia gas, the high-temperature flue gas and the original flue gas are fully mixed for the second time, and an injection grid is saved. Because of the reduction of the ammonia spraying position, the number of the stairs of the maintenance platform is reduced, and meanwhile, the function of online maintenance can be achieved by arranging the standby spray gun mounting seat.
The source of the above-mentioned raw materials is not particularly limited in the present invention, and may be generally commercially available.
In order to further illustrate the invention, the following describes a medium-low temperature SCR denitration ammonia injection system provided by the invention in detail with reference to the examples, but they should not be construed as limiting the scope of the invention.
Example 1
The medium-low temperature SCR denitration ammonia spraying system provided by the invention is applied to a certain coke oven flue gas SCR denitration system. The smoke amount of the coke oven smoke is 134640m3The NOx content in the coke oven smoke is 600mg/Nm3The temperature of the coke oven gas is 110 ℃.
The medium-low temperature SCR denitration ammonia spraying system adopts a system flow as shown in figure 2, and comprises the following steps:
an ammonia water storage tank 2 (the concentration of ammonia water is 20 wt%);
the spray gun 3 is connected with an ammonia outlet of the ammonia water storage tank;
the two-stage rotational flow ammonia spraying evaporation device 4 is connected with the outlet of the spray gun, and the bottom of the two-stage rotational flow ammonia spraying evaporation device is provided with a high-temperature flue gas inlet;
a hot blast stove 5 (the temperature of the high-temperature flue gas discharged by the hot blast stove is 800 ℃) with the high-temperature flue gas outlet connected with the high-temperature flue gas inlet of the two-stage rotational flow ammonia spraying evaporation device;
a mixer 6 with an ammonia-containing flue gas inlet connected with the flue gas outlet of the two-stage rotational flow ammonia spraying evaporation device; the mixer is also provided with an original flue gas inlet;
a flue gas heat exchanger 1 (the temperature of the coke oven flue gas is raised to 230 ℃ after passing through the flue gas heat exchanger 1) with a hot flue gas outlet connected with a raw flue gas inlet of the mixer;
the flue gas inlet is connected with the flue gas outlet of the mixer, and the SCR denitration reactor 7 is connected with the flue gas outlet of the mixer; and a flue gas outlet of the SCR denitration reactor is connected with a hot flue gas inlet of the flue gas heat exchanger.
The two-stage rotational flow ammonia injection evaporation device adopts a two-stage rotational flow ammonia injection evaporation device as shown in figure 3, and comprises:
a cavity;
the bottom to the top of cavity set gradually: a divergent section (diameter of the lower surface is 0.8m and height is 0.61m), a mixed section (diameter of 1m and height of 4.8m) and a convergent section (diameter of the upper surface is 0.7m and height is 0.61 m);
a first-stage rotational flow device is arranged at the divergent section (as shown in figure 5); the diameter of the first inner ring support 4-1-1 is 0.15m, the first sealing plate 4-1-5 is in threaded connection with the first inner ring support 4-1-1 and is used for sealing a central hole of the first inner ring support 4-1-1, and the diameter of the first outer ring support 4-1-3 is 0.6 m; the distance from the first-stage cyclone device to the bottom of the divergent section is 0.35 times of the distance from the divergent section; the number of the first rotational flow blades is 8, and the number of the first supporting blades is 8; the inclination angle between the first swirl vane and the first inner ring support axis is 45 degrees, and the included angle between the first support vane and the first swirl vane is 45 degrees.
A secondary cyclone device is arranged at the mixing section (as shown in figure 6); the diameter of the second inner ring support 4-2-1 is 0.15m, the second sealing plate 4-2-5 is in threaded connection with the second inner ring support 4-2-1 and is used for sealing a central hole of the second inner ring support 4-2-1, and the diameter of the second outer ring support 4-2-3 is 0.6 m; the distance from the secondary cyclone device to the top of the mixing section is 0.7 times of the equivalent diameter of the mixing section; the number of the second rotational flow blades is 8, and the number of the second support blades is 8; the inclination angle between the second swirl vane and the second inner ring support axis is 45 degrees, and the included angle between the second support vane and the second swirl vane is 45 degrees.
The bottom of the cavity is provided with a high-temperature flue gas inlet; the top of the cavity is provided with a smoke outlet;
two ammonia spraying ports (one for one) are arranged on the side wall of the cavity of the mixing section, each ammonia spraying port is provided with a spray gun, and the spray guns are fixed on the ammonia spraying ports through spray gun mounting seats. The distance from the ammonia spraying port to the bottom of the mixing section is 0.2 times of the equivalent diameter of the mixing section.
By adopting the double-stage rotational flow ammonia spraying evaporation device, simulation analysis shows that the flue gas temperature distribution at 500mm position above the first layer catalyst layer of the SCR denitration reactor 7 can be realized within the range of 523-531K (namely 250-258 ℃), the system meets the requirement that the temperature distribution deviation is less than +/-5 ℃, the resistance of the double-stage rotational flow ammonia spraying evaporation device to denitration flue gas is only 7Pa, the resistance generated by the double-stage rotational flow ammonia spraying evaporation device to denitration flue gas is very low, and the ammonia water evaporation and mixing effects are good. After treatment, the NOx in the original smoke is controlled to be 600mg/Nm3Down to 50mg/Nm3Hereinafter, the denitration efficiency was 92% or more.
Example 2
The medium-low temperature SCR denitration ammonia spraying system provided by the invention is applied to a certain coke oven flue gas SCR denitration system. The flue gas amount of the coke oven flue gas is 204302m3The NOx content in the coke oven smoke is 600mg/Nm3The temperature of the coke oven gas is 110 ℃.
The medium-low temperature SCR denitration ammonia spraying system adopts a system flow as shown in figure 2, and comprises the following steps:
an ammonia water storage tank 2 (the concentration of ammonia water is 20 wt%);
the spray gun 3 is connected with an ammonia outlet of the ammonia water storage tank;
the two-stage rotational flow ammonia spraying evaporation device 4 is connected with the outlet of the spray gun, and the bottom of the two-stage rotational flow ammonia spraying evaporation device is provided with a high-temperature flue gas inlet;
a hot blast stove 5 (the temperature of the high-temperature flue gas discharged by the hot blast stove is 800 ℃) with the high-temperature flue gas outlet connected with the high-temperature flue gas inlet of the two-stage rotational flow ammonia spraying evaporation device;
a mixer 6 with an ammonia-containing flue gas inlet connected with the flue gas outlet of the two-stage rotational flow ammonia spraying evaporation device; the mixer is also provided with an original flue gas inlet;
a flue gas heat exchanger 1 (the temperature of the coke oven flue gas is raised to 230 ℃ after passing through the flue gas heat exchanger 1) with a hot flue gas outlet connected with a raw flue gas inlet of the mixer;
the flue gas inlet is connected with the flue gas outlet of the mixer, and the SCR denitration reactor 7 is connected with the flue gas outlet of the mixer; and a flue gas outlet of the SCR denitration reactor is connected with a hot flue gas inlet of the flue gas heat exchanger.
The two-stage rotational flow ammonia injection evaporation device adopts a two-stage rotational flow ammonia injection evaporation device as shown in figure 3, and comprises:
a cavity;
the bottom to the top of cavity set gradually: a divergent section (diameter of the lower surface is 0.9m and height is 0.711m), a mixed section (diameter of 1.3m and height of 4.8m) and a convergent section (diameter of the upper surface is 0.9m and height is 0.61 m);
a first-stage rotational flow device is arranged at the divergent section (as shown in figure 5); the diameter of the first inner ring support 4-1-1 is 0.15m, the first sealing plate 4-1-5 and the first inner ring support 4-1-1 are in threaded welding and used for sealing a central hole of the first inner ring support 4-1-1, and the diameter of the first outer ring support 4-1-3 is 0.8 m; the distance from the first-stage cyclone device to the bottom of the divergent section is 0.35 times of the distance from the divergent section; the number of the first rotational flow blades is 8, and the number of the first supporting blades is 8; the inclination angle between the first swirl vane and the first inner ring support axis is 45 degrees, and the included angle between the first support vane and the first swirl vane is 45 degrees.
A secondary cyclone device is arranged at the mixing section (as shown in figure 6); the diameter of the second inner ring support 4-2-1 is 0.15m, the second sealing plate 4-2-5 is welded with the second inner ring support 4-2-1 and used for sealing the central hole of the second inner ring support 4-2-1, and the diameter of the second outer ring support 4-2-3 is 0.8 m; the distance from the secondary cyclone device to the top of the mixing section is 0.8 times of the equivalent diameter of the mixing section; the number of the second rotational flow blades is 8, and the number of the second support blades is 8; the inclination angle between the second swirl vane and the second inner ring support axis is 45 degrees, and the included angle between the second support vane and the second swirl vane is 45 degrees.
The bottom of the cavity is provided with a high-temperature flue gas inlet; the top of the cavity is provided with a smoke outlet;
two ammonia spraying ports (one for one) are arranged on the side wall of the cavity of the mixing section, each ammonia spraying port is provided with a spray gun, and the spray guns are fixed on the ammonia spraying ports through spray gun mounting seats. The distance from the ammonia spraying port to the bottom of the mixing section is 0.15 times of the equivalent diameter of the mixing section.
By adopting the double-stage rotational flow ammonia spraying evaporation device, simulation analysis shows that the flue gas temperature distribution at 500mm position of the upper part of the first layer catalyst layer of the SCR denitration reactor 7 can be within 523-533K (namely 250-260 ℃), the system meets the requirement that the temperature distribution deviation is less than +/-5 ℃, the resistance of the double-stage rotational flow ammonia spraying evaporation device to denitration flue gas is only 22Pa, the resistance generated by the double-stage rotational flow ammonia spraying evaporation device to denitration flue gas is very low, and the ammonia water evaporation and mixing effects are good. After treatment, the NOx in the original smoke is controlled to be 600mg/Nm3Down to 50mg/Nm3Hereinafter, the denitration efficiency was 92% or more.
The two-stage rotational flow ammonia spraying evaporation device provided by the embodiment of the invention can effectively realize the rapid evaporation and gasification of ammonia water, and the ammonia water is fully mixed with high-temperature flue gas, and the ammonia water and the raw flue gas can uniformly realize temperature rise through the flue gas mixer, so that the large temperature gradient and the thermal stress difference in an SCR inlet flue are avoided, and the temperature deviation of the mixed flue gas in the final SCR denitration reactor can meet the requirement of +/-5 ℃ and is far higher than the existing standard requirement.
In addition, the invention does not need to use an evaporator (or other evaporation devices) and a jet grid, further realizes the gasification of the ammonia water through a unique two-stage rotational flow ammonia-spraying evaporation device, and fully mixes the ammonia water with high-temperature flue gas, improves the denitration efficiency, has simple structure and low position of the ammonia-spraying device, solves the problem of difficult maintenance, and has simple and easy operation and lower cost.
The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention. Thus, the present invention is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (10)
1. A medium and low temperature SCR denitration ammonia injection system comprises:
an ammonia water storage tank;
the spray gun is connected with an ammonia outlet of the ammonia water storage tank;
the two-stage rotational flow ammonia spraying evaporation device is connected with the outlet of the spray gun, and the bottom of the two-stage rotational flow ammonia spraying evaporation device is provided with a high-temperature flue gas inlet;
the high-temperature flue gas outlet is connected with the high-temperature flue gas inlet of the two-stage rotational flow ammonia spraying evaporation device;
the mixer is connected with the ammonia-containing flue gas inlet and the flue gas outlet of the two-stage rotational flow ammonia spraying evaporation device; the mixer is also provided with an original flue gas inlet;
the hot flue gas outlet is connected with the raw flue gas inlet of the mixer;
the flue gas inlet is connected with the flue gas outlet of the mixer; and a flue gas outlet of the SCR denitration reactor is connected with a hot flue gas inlet of the flue gas heat exchanger.
2. The dual stage cyclonic ammonia injection evaporation apparatus of claim 1, wherein the dual stage cyclonic ammonia injection evaporation apparatus comprises:
a cavity;
the bottom to the top of cavity set gradually: a divergent section, a mixing section and a convergent section;
a first-stage rotational flow device is arranged on the divergent section;
a second-stage rotational flow device is arranged at the mixing section;
the bottom of the cavity is provided with a high-temperature flue gas inlet; the top of the cavity is provided with a smoke outlet;
and an ammonia spraying port is arranged on the side wall of the cavity of the mixing section.
3. The two-stage cyclone ammonia-spraying evaporation device of claim 2, wherein the distance of the divergent section is 0.1-1 times the equivalent diameter of the mixing section;
the distance between the mixing sections is 2-5 times of the equivalent diameter of the mixing sections;
the distance of the reducing section is 0.1-1 times of the equivalent diameter of the mixing section.
4. The dual stage cyclonic ammonia injection evaporation device of claim 2, wherein the primary cyclone device comprises a first inner ring support (4-1-1), first cyclone vanes (4-1-2), a first outer ring support (4-1-3), first support vanes (4-1-4) and a first closing plate (4-1-5);
the first inner ring support (4-1-1) and the first outer ring support (4-1-3) are coaxially arranged, the first rotational flow blades (4-1-2) are uniformly distributed in the area between the first inner ring support (4-1-1) and the first outer ring support (4-1-3) along the circumferential direction by taking the first inner ring support (4-1-1) as an axis, and two ends of the first rotational flow blades (4-1-2) are fixedly connected to the first inner ring support (4-1-1) and the first outer ring support (4-1-3) respectively; the inclination angles of the first rotational flow blades (4-1-2) and the first inner ring support (4-1-1) are 10-80 degrees, and the blade inclination angles of the first rotational flow blades (4-1-2) are all equal;
the first supporting blades (4-1-4) are uniformly distributed on one side, far away from the first swirl blades (4-1-2), of the first outer ring support (4-1-3) along the circumferential direction; the first supporting blade (4-1-4) is positioned on a plane formed by the first inner ring support (4-1-1) and the first outer ring support (4-1-3); one side of the first supporting blade (4-1-4) close to the first outer ring support (4-1-3) is fixedly connected with the first outer ring support (4-1-3); one side of the first supporting blade (4-1-4) far away from the first outer ring support (4-1-3) is fixedly connected with the side wall of the cavity of the divergent section;
the first sealing plate (4-1-5) is in threaded connection with the first inner ring support (4-1-1); or the first closing plate (4-1-5) is welded with the first inner ring support (4-1-1).
5. The two-stage cyclone ammonia-spraying evaporation device of claim 4, wherein the number of the first cyclone blades is 3-18;
the number of the first supporting blades is 3-16.
6. The dual-stage cyclonic ammonia injection evaporation device of claim 4, wherein the included angle between the first support blade and the first cyclonic blade is 0 ° to 180 °.
7. The dual stage cyclonic ammonia injection evaporation device of claim 2, wherein the secondary cyclone device comprises a second inner ring support (4-2-1), second cyclone vanes (4-2-2), a second outer ring support (4-2-3), second support vanes (4-2-4) and a second closing plate (4-2-5);
the second inner ring support (4-2-1) and the second outer ring support (4-2-3) are coaxially arranged, the second swirl vanes (4-2-2) are uniformly distributed in the area between the second inner ring support (4-2-1) and the second outer ring support (4-2-3) along the circumferential direction by taking the second inner ring support (4-2-1) as an axis, and two ends of each second swirl vane (4-2-2) are fixedly connected to the second inner ring support (4-2-1) and the second outer ring support (4-2-3) respectively; the inclination angles of the second swirl blades (4-2-2) and the second inner ring support (4-2-1) are 10-80 degrees, and the blade inclination angles of the second swirl blades (4-2-2) are all equal;
the second supporting blades (4-2-4) are uniformly distributed on one side, far away from the second swirl blades (4-2-2), of the second outer ring support (4-2-3) along the circumferential direction; the second supporting blade (4-2-4) is positioned on a plane formed by the second inner ring support (4-2-1) and the second outer ring support (4-2-3); one side of the second supporting blade (4-2-4) close to the second outer ring support (4-2-3) is fixedly connected with the second outer ring support (4-2-3); one side of the second supporting blade (4-2-4) far away from the second outer ring support (4-2-3) is fixedly connected with the side wall of the cavity of the mixing section;
the second sealing plate (4-2-5) is in threaded connection with the second inner ring support (4-2-1); or the second closing plate (4-2-5) is welded with the second inner ring support (4-2-1).
8. The dual-stage cyclone ammonia-injection evaporation device of claim 7, wherein the number of the second cyclone blades is 3-18;
the number of the second supporting blades is 3-16.
9. The dual-stage cyclonic ammonia injection evaporation device of claim 4, wherein the angle between the second support blade and the second cyclonic blade is 0 ° to 180 °.
10. The two-stage cyclone ammonia-spraying evaporation device of claim 2, wherein the number of the ammonia-spraying openings is the same as the number of the spray guns;
the spray gun is fixed on the ammonia spraying port through a spray gun mounting seat;
the number of the spray guns is 2-3.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113144642A (en) * | 2021-03-16 | 2021-07-23 | 北京工大环能科技有限公司 | Device for evaporation pyrolysis |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103657411A (en) * | 2013-12-13 | 2014-03-26 | 哈尔滨锅炉厂有限责任公司 | Vortex mixing device for SCR (silicon controlled rectification) flue gas denitration system |
| WO2017045602A1 (en) * | 2015-09-15 | 2017-03-23 | 中冶焦耐(大连)工程技术有限公司 | Coke oven flue gas desulfurization and denitrification combined purification process and apparatus |
| WO2017071515A1 (en) * | 2015-10-29 | 2017-05-04 | 清华大学 | Device and method enabling industrial coal-fired boiler to concurrently absorb nox and so2 |
| CN107694305A (en) * | 2017-09-19 | 2018-02-16 | 华电电力科学研究院 | A kind of SCR denitration system and its method of work of two-stage reactor series connection |
| CN108939914A (en) * | 2018-09-12 | 2018-12-07 | 国网辽宁省电力有限公司电力科学研究院 | A kind of SCR denitrating flue gas classification rotational flow mixing device |
| CN109381997A (en) * | 2018-11-06 | 2019-02-26 | 清华大学 | A kind of flue gas temperature adjustment gametic fertility integral system |
| CN209406056U (en) * | 2018-11-15 | 2019-09-20 | 中国联合工程有限公司 | Sintering flue gas denitrification apparatus |
| CN212758041U (en) * | 2020-07-03 | 2021-03-23 | 福建龙净脱硫脱硝工程有限公司 | Medium and low temperature SCR denitration ammonia injection system |
-
2020
- 2020-07-03 CN CN202010636600.2A patent/CN111632492A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103657411A (en) * | 2013-12-13 | 2014-03-26 | 哈尔滨锅炉厂有限责任公司 | Vortex mixing device for SCR (silicon controlled rectification) flue gas denitration system |
| WO2017045602A1 (en) * | 2015-09-15 | 2017-03-23 | 中冶焦耐(大连)工程技术有限公司 | Coke oven flue gas desulfurization and denitrification combined purification process and apparatus |
| WO2017071515A1 (en) * | 2015-10-29 | 2017-05-04 | 清华大学 | Device and method enabling industrial coal-fired boiler to concurrently absorb nox and so2 |
| CN107694305A (en) * | 2017-09-19 | 2018-02-16 | 华电电力科学研究院 | A kind of SCR denitration system and its method of work of two-stage reactor series connection |
| CN108939914A (en) * | 2018-09-12 | 2018-12-07 | 国网辽宁省电力有限公司电力科学研究院 | A kind of SCR denitrating flue gas classification rotational flow mixing device |
| CN109381997A (en) * | 2018-11-06 | 2019-02-26 | 清华大学 | A kind of flue gas temperature adjustment gametic fertility integral system |
| CN209406056U (en) * | 2018-11-15 | 2019-09-20 | 中国联合工程有限公司 | Sintering flue gas denitrification apparatus |
| CN212758041U (en) * | 2020-07-03 | 2021-03-23 | 福建龙净脱硫脱硝工程有限公司 | Medium and low temperature SCR denitration ammonia injection system |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113144642A (en) * | 2021-03-16 | 2021-07-23 | 北京工大环能科技有限公司 | Device for evaporation pyrolysis |
| CN113144642B (en) * | 2021-03-16 | 2024-03-26 | 北京紫黄科技有限公司 | Device for evaporation pyrolysis |
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